Fuel cells with improved resistance to fuel crossover

ABSTRACT

The invention provides a fuel cell comprising an anode in an anode region of the cell and a cathode in a cathode region of the cell, the anode being separated from the cathode by an ion selective polymer electrolyte membrane, the anode region of the cell being supplied in use thereof with an alcoholic fuel, the cathode region of the cell being supplied in use thereof with an oxidant, the cell being provided with means for generating an electrical circuit between the anode and the cathode and with a non-volatile redox couple in solution in flowing fluid communication with the cathode in the cathode region of the cell, the redox couple being at least partially reduced at the cathode in operation of the cell, and at least partially regenerated by reaction with the oxidant after such reduction at the cathode.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of Application Ser. No. 12/298,355,which is the National Stage of International Application No.PCT/GB2007/050211, filed Apr. 24, 2007, which was published in Englishas International Publication No. WO 2007/122431 on Nov. 1, 2007, andclaims the benefit of GB 0608079.0 filed Apr. 25, 2006.

BACKGROUND

1. Field

The present invention relates to fuel cells, in particular to fuel cellsin operation of which an alcohol is supplied as fuel to the anode regionof the cell. Such cells have applications in microfuel cells forelectronic and portable electronic components, and also in larger fuelcells for the automotive industry.

2. Description of the Related Art

A fuel cell is an electrochemical energy conversion device that convertsfuel and oxidant into reaction products, producing electricity and heatin the process. In one example of such a cell, methanol is used as fuel,and air or oxygen as oxidant, and the products of the reaction arecarbon dioxide and water. The electrochemical reactions in this cell inoperation may be summarised as follows:

Anode CH₃OH+H₂O

CO₂+6H⁺+6e⁻

Cathode 3/2O₂+6H⁺+6e⁻

3H₂O

Overall CH₃OH+_(3/2)O₂

CO₂+2H₂O

The methanol fuel and oxidant are fed respectively into catalysing,diffusion-type electrodes separated by an electrolytic membrane whichallows the passage of protons from the anode chamber to the cathodechamber to balance the cathode reaction. The electrons generated in theanode chamber flow in an external electrical circuit and are returned tothe cathode having provided the power output from the cell. Such fuelcells are known as direct methanol fuel cells (DMFCs). Various types ofmembrane may be used, such as polymer electrolyte membranes (PEMs),comprising for example Nafion™. Fuel cells based on polymer electrolytemembranes (PEM fuel cells) are convenient for portable applications suchas portable electronics and automotive technology due to theirrelatively low temperatures of operation. Further or alternativeadaptations to the PEM barrier include the provision of a bimembrane asdescribed in our co-pending application PCT/EP2006/060640.

WO-A-2006/012637 discloses a reactor and corresponding method forproducing electrical energy using a fuel cell by selectively oxidisingCO at room temperature using polyoxometallate compounds.

US-A-2005/0112055 discloses a catalyst comprisingdi-ruthenium-substituted polyoxometallate and a method of using theelectrocatalyst to generate oxygen. US-A-2004/0137297 discloses an ionexchange membrane said to be useful for the diaphragm of a directmethanol type fuel cell.

Methanol and other low molecular weight alcohols are convenient fuelsfor portable fuel cells because their energy density is relatively high,eg, for methanol, six moles of electrons being generated in theelectrochemical half cell for every mole of fuel consumed. However,DMFCs typically suffer from crossover effects—methanol is transportedacross the membrane by diffusion and electro-osmosis. This causes areduction in the performance of the fuel cell by the effect of methanolbeing oxidized at the cathode, typically comprising Pt or other noblemetal catalyst. Here the methanol is oxidized at the potentials ofoxygen reduction. The potential and current are reduced, causing a lossin power density; the open circuit potential is also reduced.

Conventionally, routes to reduce the methanol crossover effect haveincluded:

-   -   i) Increasing the membrane thickness—typically 170 μm Nafion is        used instead of the more common 50 μm membrane for hydrogen fuel        cells. This increases the resistance of the membrane—whilst not        completely eliminating the crossover impact.    -   ii) Using an alternative membrane to the Nafion-type sulphonated        fluoropolymer. Usually these membranes require higher        temperatures (>100° C.) to operate effectively, or conduct less        well or swell.    -   iii) Using selective catalysts for the cathode. These are        generally poorer catalysts for oxygen reduction than noble        metal-containing catalysts such as Pt and Pt-containing        catalysts.

The phenomenon of methanol crossover and potential solutions have beenreviewed recently.

-   -   International activities in DMFC R&D: status of technologies and        potential applications, R Dillon, S Sriinivasan, A S Arico, V        Antonucci, J Power Sources, 127, 112 (2004).    -   M P Hogarth, T R Ralph, Platinum Metal Reviews, 46, 146 (2002).    -   A Heinzel, V M Barragan, J Power Sources, 84,70 (1999).

SUMMARY

It is an object of the present invention to provide an improvedalcohol-fuelled fuel cell. In particular, it is intended overcome orameliorate one or more of the aforesaid disadvantages caused bycrossover of the alcoholic fuel across the membrane separating the anodefrom the cathode. It is a more specific object of the invention toreduce the impact of crossover of direct methanol or other alcohol fuelcells whilst being able to operate at a temperature below that requiringapplied pressure, and without unsatisfactorily compromising cellperformance.

According to the present invention there is provided a fuel cellcomprising an anode in an anode region of the cell and a cathode in acathode region of the cell, the anode being separated from the cathodeby an ion selective polymer electrolyte membrane, the anode region ofthe cell being supplied in use thereof with an alcoholic fuel, thecathode region of the cell being supplied in use thereof with anoxidant, the cell being provided with means for generating an electricalcircuit between the anode and the cathode and with a non-volatile redoxcouple in solution in flowing fluid communication with the cathode inthe cathode region of the cell, the redox couple being at leastpartially reduced at the cathode in operation of the cell, and at leastpartially re-generated by reaction with the oxidant after such reductionat the cathode, the redox couple and/or the concentration of the redoxcouple in the catholyte solution being selected so that the currentdensity for a given potential generated by the cell in operation issubstantially unaffected by the oxidation of alcoholic fuel due tocrossover from the anode region of the cell to the cathode region of thecell across the polymer electrolyte membrane,

By “substantially unaffected” is preferably meant that the currentdensity, for any given potential, of alcoholic fuel oxidation at thecathode when the cell in operation at a particular temperature is lessthan about 10%, more preferably less than about 5%, most preferably byless than about 1% over a period of time during which crossover of fuelacross the polymer electrolyte membrane occurs.

A fuel cell in accordance with the invention may conveniently be testedfor compliance with these and the following criteria by test doping thecathode region of the cell with the alcoholic fuel, for example at aconcentration of alcoholic fuel in the doped catholyte solutioncomparable to that found due to crossover of fuel from the anode.

A fuel cell is provided in accordance with the invention in which thecurrent density for any given potential due to oxidation of thealcoholic fuel is less than about 10%. more preferably less than about5% and mostre preferably less than about 1% when the cathode chamber issupplied with alcoholic fuel at a concentration comparable to thatcreated by crossover.

In one embodiment, the fuel cell is fitted with a switchable electronicvalve that allows reverse flow of electrons along a connecting line inthe circuit when electromotive force is supplied to the fuel cell.

The invention therefore provides a cathode regenerative redox flowsystem comprising a liquid flowing catholyte solution and a chamber forthe regeneration of a redox species consumed at the electrode by oxygen.Surprisingly this has been found to reduce the impact of alcohol fuel,eg methanol, crossover. Without wishing to be limited by theory, itappears that methanol is effectively inactive at the cathode, enablingthe catholyte redox species to be unimpeded in its reduction at thecathode.

In operation the fuel cell will usually provide electromotive force tosome external mechanism (the drive shaft of an automobile or theprocessor of an electronic component, for example).

Suitable fuels include low molecular weight alcohols such as methanol,ethanol, propanol, isopropanol and butanol, dipropylene glycol andethylene glycol.

Suitable oxidant gas materials include oxygen and air and hydrogenperoxide.

Preferably the anode electrode comprises a diffusion layer and anelectrocatalyst layer. The diffusion layer is suitably of a graphiticnature, and the electrocatalyst layer is suitably of finely dividedplatinum or palladium. Platinum based alloys are also suitable for usein one or both electrodes, the alloy metal being suitably selected fromtin, iridium, osmium, rhenium or ruthenium. Generally speaking, thechoice of alloy depends on the fuel to be oxidised at the anodeelectrode. Platinum-ruthenium alloy anodes are preferable forelectro-oxidation of methanol, for example.

The cathode in the redox fuel cell of the invention may comprise ascathodic material carbon, platinum, nickel, metal oxide species.However, it is preferable that expensive cathodic materials are avoided,and therefore preferred cathodic materials include carbon, nickel, metaloxide. The cathodic material may be constructed from a fine dispersionof particulate cathodic material, the particulate dispersion being heldtogether by a suitable adhesive, or simply by the proton conductingpolymeric material. The cathode is designed to create maximum flow ofredox mediator to the cathode surface. Thus it may consist of shapedflow regulators or a three dimensional electrode; the liquid flow may bemanaged in a flow-by arrangement where there is a liquid channeladjacent to the electrode, or in the case of the three dimensionalelectrode, where the liquid is forced to flow through the electrode. Itis intended that the surface of the electrode is also theelectrocatalyst, but it may be beneficial to adhere the electrocatalystin the form of deposited particles on the surface of the electrode.

Transition metal ions, and complexes of transition metal ions formsuitable redox couples for use in the fuel cell of the invention.Suitable transition metals include vanadium, molybdenum, iron, manganeseand copper. One example of a suitable redox couple is the ferrous/ferricphenanthroline complex. Other examples include polyoxometallates. In onefuel cell of the invention, the redox couple comprises apolyoxometallate species. In this case the catholyte solution preferablycomprises at least about 0.1 M of a polyoxometallate.

The polyoxometallate when used as the redox species may be representedby the formula:

X_(a)[Z_(b)M_(c)O_(d)]

wherein:

X is selected from hydrogen, alkali metals, alkaline earth metals,ammonium and combinations of two or more thereof:

Z is selected from B, P, S, As, Si, Ge, Ni, Rh, Sn, Al, Cu, I, Br, F,Fe, Co, Cr, Zn,

H₂, Te, Mn and Se and combinations of two or more thereof;

M is a metal selected from Mo, W, V, Nb, Ta, Mn, Fe, Co, Cr, Ni, Zn Rh,Ru, Tl, Al, Ga, In and other metals selected from the 1^(st) ,2nd and3^(rd) transition metal series and the lanthanide series, andcombinations of two or more thereof;

a is a number of X necessary to charge balance the [M_(c)O_(d)] anion;

b is from 0 to 20, more preferably 0-2

c is from 1 to 40; and

d is from 1 to 180.

Vanadium and molybdenum, and combinations thereof, are particularlypreferred for M.

Phosphorus is particularly preferred for Z.

A combination of hydrogen and an alkali metal and/or alkaline earthmetal is particularly preferred for X. One such preferred combination ishydrogen and sodium.

Specific examples of polyoxometallates include molybdophosphoric acid,H₃PMo₁₂ O₄₀ and molybdovanadophosphosphoric acid, H₅PMo₁₀V₂O₄₀.

Thus, according to a first aspect of the present invention, there isprovided a fuel cell in accordance with the invention wherein thecatholyte solution comprises a polyoxometallate catalyst. In a preferredembodiment of the present invention, the catalyst comprises vanadium Ina more preferred embodiment, the catalyst comprises vanadium andmolybdenum. In a preferred embodiment of the present invention, thepolyoxometallate comprises vanadium, more preferably vanadium andmolybdenum. Thus, the catalyst may be H₃Na₂PMo₁₀V₂O₄₀. Alternatively,the catalyst may be H₃Na₃PMo₉V₃O₄₀ or H₃Na₄PMo₈V₄O₄₀ and compounds ofintermediate composition. In addition, a mixture of these or otherpolyoxometallate catalysts is also envisaged. For this embodiment,preferably, at least one X is hydrogen. However, it is also preferredthat not all X be hydrogen.

More preferably, at least two of X are not hydrogen. X comprising atleast one hydrogen and at least one other material selected from alkalimetals, alkaline earth metals, ammonium and combinations of two or morethereof is preferred.

The concentration of the polyoxometallate in the catholyte solution ispreferably at least about 0.1M, preferably at least about 0.15M, morepreferably at least about 0.175M and most preferably at least about0.2M.

Accordingly, the present invention provides a redox fuel cell comprisingan anode and a cathode separated by an ion selective polymer electrolytemembrane: means for supplying an alcoholic fuel to the anode region ofthe cell; means for supplying an oxidant to the cathode region of thecell; means for providing an electrical circuit between the anode andthe cathode; a solution containing non-volatile catholyte componentsflowing in fluid communication with the cathode, the catholyte solutioncomprising a redox couple being at least partially reduced at thecathode in operation of the cell, and at least partially re-generated byreaction with the oxidant after such reduction at the cathode, thecatholyte solution comprising at least about 0.1M of the said redoxcouple.

In one preferred embodiment of the invention, the ion selective PEM is acation selective membrane which is selective in favour of protons versusother cations.

The cation selective polymer electrolyte membrane may be formed from anysuitable material, but preferably comprises a polymeric substrate havingcation exchange capability. Suitable examples include fluororesin-typeion exchange resins and non-fluororesin-type ion exchange resins.Fluororesin-type ion exchange resins include perfluorocarboxylic acidresins, perfluorosulfonic acid resins, and the like. Perfluorocarboxylicacid resins are preferred, for example “Nafion” (Du Pont Inc.),“Flemion” (Asahi Gas Ltd),“Aciplex” (Asahi Kasei Inc), and the likeNon-fluororesin-type ion exchange resins include polyvinylalcohols,polyalkylene oxides, styrene-divinylbenzene ion exchange resins, and thelike, and metal salts thereof. Preferred non-fluororesin-type ionexchange resins include polyalkylene oxide-alkali metal salt complexes.These are obtainable by polymerizing an ethylene oxide oligomer in thepresence of lithium chlorate or another alkali metal salt, for example.Other examples include phenolsulphonic acid, polystyrene sulphonic,polytriflurostyrene sulphonic, sulphonated trifluorostyrene, sulphonatedcopolymers based on α,β,β-triflurostyrene monomer, radiation-graftedmembranes. Non-fluorinated membranes include sulphonatedpoly(phenylquinoxalines), poly (2,6 diphenyl-4-phenylene oxide),poly(arylether sulphone), poly(2,6-diphenylenol); acid-dopedpolybenzimidazole, sulphonated polyimides;styrene/ethylene-butadiene/styrene triblock copolymers; partiallysulphonated polyarylene ether sulphone; partially sulphonated polyetherether ketone (PEEK); and polybenzyl suphonic acid siloxane (PBSS).

In some cases it may be desirable for the ion selective polymerelectrolyte membrane to comprise a bi-membrane. The bimembrane ifpresent will generally comprise a first cation selective membrane and asecond anion selective membrane. In this case the bimembrane maycomprise an adjacent pairing of oppositely charge selective membranes.For example the bi-membrane may comprise at least two discreet membraneswhich may be placed side-by-side with an optional gap therebetween.Preferably the size of the gap, if any, is kept to a minimum in theredox cell of the invention. The use of a bi-membrane may be used in theredox fuel cell of the invention to maximise the potential of the cell,by maintaining the potential due to a pH drop between the anode andcatholyte solution. Without being limited by theory, in order for thispotential to be maintained in the membrane system, at some point in thesystem, protons must be the dominant charge transfer vehicle. A singlecation-selective membrane may not achieve this to the same extent due tothe free movement of other cations from the catholyte solution In themembrane.

In this case the cation selective membrane may be positioned on thecathode side of the bimembrane and the anion selective membrane may bepositioned on the anode side of the bimembrane. In this case, the cationselective membrane is adapted to allow protons to pass through themembrane from the anode side to the cathode side thereof in operation ofthe cell. The anion selective membrane is adapted substantially toprevent cationic materials from passing therethrough from the cathodeside to the anode side thereof, although in this case anionic materialsmay pass from the cathode side of the anionic-selective membrane to theanode side thereof, whereupon they may combine with protons passingthrough the membrane in the opposite direction. Preferably the anionselective membrane is selective for hydroxyl ions, and combination withprotons therefore yields water as product.

In a second embodiment of the invention the cation selective membrane ispositioned on the anode side of the bimembrane and the anion selectivemembrane is positioned on the cathode side of the bi-membrane. In thiscase, the cation selective membrane is adapted to allow protons to passthrough the membrane from the anode side to the cathode side thereof inoperation of the cell. In this case, anions can pass from the cathodeside into the interstitial space of the bimembrane, and protons willpass from the anode side. It may be desirable in this case to providemeans for flushing such protons and anionic materials from theinterstitial space of the bimembrane. Such means may comprises one ormore perforations in the cation selective membrane, allowing suchflushing directly through the membrane. Alternatively means may beprovided for channelling flushed materials around the cation selectivemembrane from the interstitial space to the cathode side of the saidmembrane.

According to another aspect of the present invention, there is provideda method of operating a proton exchange membrane fuel cell comprisingthe steps of

a) forming H⁺ ions by the oxidation of an alcoholic fuel at an anodesituated adjacent to a proton exchange membrane;

b) supplying a catholyte comprising a non-volatile redox couple solutionin an oxidised state to a cathode situated oppositely adjacent to theproton exchange membrane; and

c) allowing the redox couple to become reduced upon contact with thecathode concomitantly with H⁺ ions passing through the membrane tobalance charge.

In a preferred embodiment, the catholyte is supplied from a catholytereservoir.

The method of the above fourth aspect may additionally comprise the stepof:

d) passing the catholyte from the cathode to a reoxidation zone whereinthe catalyst is reoxidised.

In this embodiment, the cell is cyclic and the redox couple in thecathode can be repeatedly oxidised and reduced without having to bereplaced.

BRIEF DESCRIPTION OF THE DRAWING

The invention will now be more particularly described with reference tothe following Figures and Examples, in which:

FIG. 1 a shows the I-V curves of a fuel cell in accordance with theinvention and described in Example 1 using POM (7 ml/min ˜0.9 M vanadium(V) in ˜0.3 M POM) in the cathode, 2 ml/min 1.0 M methanol in the anode,

FIG. 1 b shows the power densities of a fuel cell in accordance with theinvention and described in Example 1 using POM (7 ml/min ˜0.9 M vanadium(V) in ˜0.3 M POM) in the cathode, 2 ml/min 1.0 M methanol in the anode.

FIG. 2 shows a comparison of conventional DMFC with a POM/DMFC system(70 ml/min ˜0.3 M POM solution, 2 ml/min 1.0 M methanol, membrane:Nafion 115, anode: PtRu, cathode: RVC) in accordance with the inventionand described in Example 2.

FIG. 3 shows a blank CV experiment without POM system at 60° C., 50 mV/Swith the working electrode: 0.5 cm² RVC, CE: Platinum, RE: Ag/AgCl,described in Example 3.

FIG. 4 shows the Example 3 CV curves with different POM solution at 60°C. with a scan rate of 50 mV/S with the working electrode: 0.5 cm² RVC,CE: Platinum, RE: Ag/AgCl.

FIG. 5 shows the effect of Nafion membranes on the performance ofPOM/DMFC, 5 ml/min 1.0 M methanol, 180 ml/min 0.3M V3 POM, 500 ml intotal MEA, RVC in the cathode, cell temperature: 77° C., referred to inExample 4

FIG. 6 shows the effect of methanol concentration on the performance ofPOM/DMFC, Nafion 117, E-Tek ½ MEA, RVC in the cathode, 2 ml/minmethanol. 90 ml/min ˜0.3 M V3 POM (total around 260 ml), celltemperature: 79-81° C., referred to in Example 5.

FIG. 7 shows a schematic diagram of a fuel cell constructed and arrangedin accordance with the invention.

DETAILED DESCRIPTION

Referring to FIG. 7, there is shown the cathode and anode side of fuelcell 1 in accordance with the invention comprising a polymer electrolytemembrane 2 separating an anode 10 from cathode 3. Cathode 3 comprises inthis diagram reticulated carbon and is therefore porous. However otherporous materials such as carbon felts and similar carbon fibre-basedsystems, as well as porous metal foams and grids and metal particles andmetal oxide particles deposited on these porous materials. Polymerelectrolyte membrane 2 comprises cation selective Nafion 115 membranethrough which protons generated by the (optionally catalytic) oxidationof fuel (in this case methanol) in the anode chamber pass in operationof the cell, as schematically shown by the large arrows in FIG. 7.Electrons (e-) generated at the anode 10 by the oxidation of fuel gasflow in an electrical circuit 12 and are returned to cathode 3. Fuel 14(in this case methanol) is supplied to the fuel passage 16 from a fuelsupply 18 of the anode chamber, while the oxidant (in this case air) issupplied to oxidant inlet 4 of cathode gas reaction chamber 5. Cathodegas reaction chamber 5 (the catalyst reoxidation zone) is provided withexhaust 6, through which the by-products of the fuel cell reaction(e,g., water and heat) can be discharged. The anode chamber is alsoprovided with an exhaust for the carbon dioxide half reaction product inthe anode region.

A catholyte solution comprising a catalyst and redox couple, in thiscase the oxidised form of the polyoxometallate provides both functions,is supplied in operation of the cell from catholyte reservoir 7 into thecathode inlet channel 8. The catholyte passes into reticulated carboncathode 3, which is situated adjacent membrane 2. As the catholytepasses through cathode 3, the polyoxometallate catalyst is reduced andis then returned to cathode gas reaction chamber 5 via cathode outletchannel 9.

Due to the advantageous composition of the catholyte of the presentinvention, reoxidation of the catalyst occurs very rapidly, which allowsthe fuel cell to produce a higher sustainable current than withcatholytes of the prior art.

Fuel, for example methanol, is passed against the first electrode(anode) and, at the first electrode the following redox reaction occurs:

CH₃OH+H₂O

CO₂+6H⁺+6e⁻

Electrons generated at the first electrode flow through the circuit,whilst protons generated at the first electrode flow through the gasdiffusion substrate and through the polymer electrolyte membrane towardsthe second electrode.

The fuel cell is provided with a reservoir 8 of a redox couple, whichmay be generally indicated as [R], [R] may comprise for example aferrous/ferric phenanthroline complex or a polyoxometallate complex hashereinbefore described, or may be any other suitable redox couple. Inoperation of the cell the oxidised redox material is passed against thesecond electrode and [R]^(ox) ions are reduced to [R]^(red) ions.

[R]^(ox)+ne⁻→[R]^(red)

Water is also liberated in the gas reaction chamber in accordance withthe following equation:

(4/n)[R]^(red)+O₂+4H⁺→(4/n)[R]^(ox)+2H₂O

If peroxide is used as the oxidant instead of air or oxygen, then thereaction becomes

(2/n)[R]^(red)+H₂O₂+2H⁺→(2/n)[R]^(ox)+2H₂O

The reservoir is supplied in normal use of the cell with an oxidantmaterial (for example air).

Preferably, the redox potential of the redox couple is less than about0.6V, more preferably less than about 0.5V different from the potentialof oxygen. For example the redox potential of the redox couple may befrom about 0.01V to about 0.6V, from about 0.01V to about 0.5V, or fromabout 0.01V to about 0.3V different from the potential of oxygen.

EXAMPLE 1

A catholyte solution comprising H₃Na₂PMo₉V₃O₄₀ was prepared and chargedto the cathode chamber of a fuel cell generally in accordance with thatdescribed with reference to FIG. 7.

The membrane electrode assembly (MEA) in this experiment comprised:anode: JM PtRu black catalyst, 4.3 mg cm⁻² and 10% Nafion; cathode: 2.0mm thick RVC+carbon veil. The anode gas diffusion layer was 10%teflonized carbon paper with 2 mg cm⁻² XC-72 C and 10% Nafion; Membrane:Nafion 115; Area: 6.25 cm². Flow field: modified commercial parallelanode and sink flow field in the cathode.

As shown in FIG. 1, the performance of a redox cathode in a DMFC using aH₃Na₃PMo₉V₃O₄₀ POM system provides a maximum of power density at 80° C.of about 40 mW cm⁻², which decreases with the temperature.

EXAMPLE 2

The comparison, with reference to FIG. 2, is shown of the redox cathodecompared with a gas cathode. It can be seen that the redox cathodeperforms better, the performance of an air gas cathode at 60° C. iscomparable to the redox cathode performance at 50° C. The anode catalystlayer comprises 4 mg cm⁻² PtRu black from JM and 10 wt % Nafion inside,The anode gas diffusion layer was 10% teflonized carbon paper with 2 mgcm-2 XC-72 carbon and 10% Nafion,

EXAMPLE 3

Here, with reference to FIGS. 3 and 4, cyclic voltammetry is used tostudy the behaviour of methanol at the carbon electrode. A workingelectrode composed of 100 ppm RVC, used in the fuel cell studies wasused. Current levels due to methanol were less than +/−0.01 mA cm⁻² inthe range of potentials of operation of the fuel cell, which is anegligible current in comparison with the current densities of the fuelcell in operation. The CV of a low level of POM in the presence ofmethanol shows minimal impact in the range of operation of the fuelcell. Thus the impact of cross-over is limited at the electrode—nocounter-current due to methanol oxidation occurs and there is littleloss of the POM reduction.

EXAMPLE 4

In this example similar cell, cathode and anode construction were usedas for previous examples. FIG. 5 shows a comparison in performancebetween nafion 117 at ˜180μ and nafion 115 at ˜120μ. It is clearly shownthat the performance is better over nearly the whole current/voltagerange, in contrast to the air cathode where nafion 117 is preferred dueto the detrimental effects on performance of methanol crossover.

EXAMPLE 5

In this example, with reference to FIG. 6, was used a ½ MEA from EtekSERIES 12D-W MEA (5-layer) Half Membrane. Electrode Assembly for DMFCgeneral purpose 5-layer, GDL base on woven web, in a similar cell andcathode to earlier examples using a modified commercial serpentine flowfield for the anode. Other details are shown with the figure headings.

The benefit of using the fuel cell cathode of the invention is clear:there is no decrease in ocp with increasing methanol and little changein performance up to 8M MeOH, which contrasts strongly with aircathodes, where 1 M MeOH is preferred, and performance is weaker above 2M methanol (Heinzel).

What is claimed is:
 1. A fuel cell comprising an anode in an anoderegion of the cell and a cathode in a cathode region of the cell, theanode being separated from the cathode by an ion selective polymerelectrolyte membrane, the anode region of the cell being supplied withan alcoholic fuel, the cathode region of the cell being supplied with anoxidant, the cell being provided with means for generating an electricalcircuit between the anode and the cathode and with a non-volatile redoxcouple in solution in flowing fluid communication with the cathode inthe cathode region of the cell, the redox couple being at leastpartially reduced at the cathode in operation of the cell, and at leastpartially re-generated by reaction with the oxidant after such reductionat the cathode, the redox potential of the redox couple being from 0.01Vto 0.6V different from the potential of oxygen and the redox coupleand/or the concentration of the redox couple in the catholyte solutionbeing selected so that the current density generated by the cell inoperation is substantially unaffected by the oxidation of alcoholic fueldue to crossover of the alcoholic fuel from the anode region of the cellto the cathode region of the cell across the polymer electrolytemembrane.
 2. A fuel cell according to claim 1 wherein the alcoholic fuelis selected from methanol, ethanol, propanol, isopropanol and butanol,dipropylene glycol and ethylene glycol, and mixtures of two or morethereof.
 3. A fuel cell according to claim 1 wherein the redox potentialof the redox couple is from 0.01V to 0.3V different from the potentialof oxygen.
 4. A fuel cell according to claim 1 wherein the operatingtemperature of the fuel cell is below 100° C.
 5. A fuel cell accordingto claim 1 wherein the redox couple comprises at least one transitionmetal complex.
 6. A fuel cell according to claim 5 wherein the redoxcouple comprises a polyoxometallate species.
 7. A fuel cell according toclaim 1 wherein the concentration of the redox couple in the catholytesolution is at least about 0.1M.
 8. A fuel cell according to claim 1wherein the cathode region of the cell is provided with a reservoir forstoring the catholyte solution.
 9. A fuel cell according to claim 1wherein the fuel cell is fitted with a switchable electronic valve toallow reverse flow of electrons along the connecting line whenelectromotive force is supplied to the fuel cell.